Processing olefin copolymers

ABSTRACT

The invention is directed to essentially saturated hydrocarbon polymer composition comprising essentially saturated hydrocarbon polymers having A) a backbone chain; B) a plurality of essentially hydrocarbyl sidechains connected to A), said sidechains each having a number-average molecular weight of from 2500 Daltons to 125,000 Daltons and a MWD by SEC of 1.0-3.5; and having A) a Newtonian kimiting viscosity (η 0 ) at 190° C. at least 50% greater than that of a linear olefinic polymer of the same chemical composition and weight average molecular weight, preferably at least twice as great as that of said linear polymer, B) a ratio of the rubbery plateau modulus at 190° C. to that of a linear polymer of the same chemical composition less than 0.5, preferably &lt;0.3, C) a ratio of the Newtonian limiting viscosity (η 0 ) to the absolute value of the complex viscosity in oscillatory shear (η*)at 100 rad/sec at 190° C. of at least 5, and D) a ratio of the extensional viscosity measured at a strain rate of 1 sec −1 , 190° C., and time 3 sec (i.e., a strain of 3) to that predicted by linear viscoelasticity at the same temperature and time of 2 or greater. Ethylene-butene prepared by anionic polymerization and hydrogenation illustrate and ethylene-hexene copolymers prepared by coordination polymerization illustrate the invention. The invention polymers exhibit improved processing characteristics in that the shear thinning behavior closely approaches that of ideal polymers and exhibit improved strain thickening.

TECHNICAL FIELD

[0001] The invention relates to improved processing olefin copolymershaving a plurality of substantially linear branches and to compositionscomprising them.

BACKGROUND OF THE INVENTION

[0002] Ethylene copolymers are a well-known class of olefin copolymersfrom which various plastic products are now produced. Such productsinclude films, fibers, and such thermomolded articles as containers andcoatings. The polymers used to prepare these articles are prepared fromethylene, optionally with one or more additional copolymerizablemonomers. Low density polyethylene (“LDPF”) as produced by free radicalpolymerization consists of highly branched polymers where the branchesoccur randomly throughout the polymer, that is on any number of formedsegments or branches. The structure exhibited easy processing, that ispolymers with it could be melt processed in high volumes at low energyinput. Machinery for conducting this melt processing, for exampleextruders and film dies of various configurations, was designed intoproduct finishing manufacturing processes with optimal design featuresbased on the processing characteristics of the LDPE.

[0003] However, with the advent of effective coordination catalysis ofethylene copolymers, the degree of branching was significantlydecreased, both for the now traditional Ziegler-Natta ethylenecopolymers and those from the newer metallocene catalyzed ethylenecopolymers. Both, particularly the metallocene copolymers, areessentially linear polymers, which are more difficult to melt processwhen the molecular weight distribution (MWD=M_(w)/M_(n), where M_(w) isweight-average molecular weight and M_(n) is number-average molecularweight) is narrower than about 3.5. Thus broad MWD copolymers are moreeasily processed but can lack desirable solid state attributes otherwiseavailable from the metallocene copolymers. Thus it has become desirableto develop effective and efficient methods of improving the meltprocessing of olefin copolymers while retaining desirable meltproperties and end use characteristics.

[0004] The introduction of long chain branches into substantially linearolefin copolymers has been observed to improve processingcharacteristics of the polymers. Such has been done using metallocenepolymers where significant numbers of olefinically unsaturated chainends are produced during the polymerization reaction. See, e.g., U.S.Pat. No. 5,324,800. The olefinically unsaturated polymer chains canbecome “macromonomers” or “macromers” and, apparently, can bere-inserted with other copolymerizable monomers to form the branchedcopolymers. International publication WO 94/07930 addresses advantagesof including long chain branches in polyethylene from incorporatingvinyl-terminated macromers into polyethylene chains where the macromershave critical molecular weights greater than 3,800, or, in other wordscontain 250 or more carbon atoms. Conditions said to favor the formationof vinyl terminated polymers are high temperatures, no comonomer, notransfer agents, and a non-solution process or a dispersion using analkane diluent. Increase of temperature during polymerization is alsosaid to yield 0-hydride eliminated product, for example while addingethylene so as to form an ethylene “end cap”. This document goes on todescribe a large class of both monocyclopentadienyl andbiscyclopentadienyl metallocenes as suitable in accordance with theinvention when activated by either alumoxanes or ionizing compoundsproviding stabilizing, noncoordinating anions.

[0005] U.S. Pat. Nos. 5,272,236 and 5,278,272 describe “substantiallylinear” ethylene polymers which are said to have up to about 3 longchain branches per 1000 carbon atoms. These polymers are described asbeing prepared with certain monocyclopentadienyl transition metal olefinpolymerization catalysts, such as those described in U.S. Pat. No.5,026,798. The copolymer is said to be useful for a variety offabricated articles and as a component in blends with other polymers.EP-A-0 659 773 A1 describes a gas phase process using metallocenecatalysts said to be suitable for producing polyethylene with up to 3long chain branches per 1000 carbon atoms in the main chain, thebranches having greater than 18 carbon atoms.

[0006] Reduced melt viscosity polymers are addressed in U.S. Pat. Nos.5,206,303 and 5,294,678. “Brush” polymer architecture is described wherethe branched copolymers have side chains that are of molecular weightsthat inhibit entanglement of the backbone chain. These branchweight-average molecular weights are described to be from 0.02-2.0 M_(e)^(B), where M_(e) ^(B) is the entanglement molecular weight of the sidebranches. Though the polymers illustrated are isobutylene-styrenecopolymers, calculated entanglement molecular weights for ethylenepolymers and ethylene-propylene copolymers of 1,250 and 1,660 areprovided. Comb-like polymers of ethylene and longer alpha-olefins,having from 10 to 100 carbon atoms, are described in U.S. Pat. No.5,475,075. The polymers are prepared by copolymerizing ethylene and thelonger alpha-olefins which form the side branches. Improvements inend-use properties, such as for films and adhesive compositions aretaught.

DISCLOSURE OF THE INVENTION

[0007] The invention is directed to a polymer composition comprisingessentially saturated hydrocarbon polymers having: A) a backbone chain;B) a plurality of essentially hydrocarbon sidechains connected to A),said sidechains each having a number-average molecular weight of from2,500 Daltons to 125,000 Daltons and an MWD by SEC of 1.0- 3.5; and, C)a mass ratio of sidechains molecular mass to backbone molecular mass offrom 0.01:1 to 100:1. These invention compositions comprise essentiallysaturated hydrocarbon polymers having: A) a Newtonian limiting viscosity(,no) at 190° C. at least 50% greater than that of a linear olefinicpolymer of the same chemical composition and weight average molecularweight, preferably at least twice as great as that of said linearpolymer, B) a ratio of the rubbery plateau modulus at 190° C. to that ofa linear polymer of the same chemical composition less than 0.5,preferably <0.3, C) a ratio of the Newtonian limiting viscosity (η₀) tothe absolute value of the complex viscosity in oscillatory shear (η*) at100 rad/sec at 190° C. of at least 5, and D) a ratio of the extensionalviscosity measured at a strain rate of 1 sec⁻¹, 190° C., and time=3 sec(i.e., a strain of 3) to that predicted by linear viscoelasticity at thesame temperature and time of 2 or greater. The invention polymersexhibit highly improved processing properties, improved shear thinningproperties and melt strength.

BRIEF DESCRIPTION OF DRAWINGS

[0008] FIGS. I-IV illustrate viscometric data of an ethylene-butenecopolymer of the invention in comparison with similarly obtained datafor traditional low density polyethylene (LDPE) and metallocene lowdensity polyethylenes (LLDPE). FIG. I illustrates the complex viscosityvs. the frequency of oscillatory deformation at 190° C. FIG. IIillustrates the normalized viscosity vs. the frequency times the zeroshear viscosity at 190° C. FIG. III illustrates the storage modulus vs.the frequency at 190° C. FIG. IV illustrates the storage modulus vs. thefrequency times the zero shear viscosity at 190° C. FIG. V illustratesthe relation between the extensional viscosity (η_(ext) (linear)) andthat measured (η_(ext) (meas)) for a polymer that shows significantstrain hardening.

DETAILED DESCRIPTION OF THE INVENTION

[0009] The branched hydrocarbon copolymers according to the inventioncan be described as those having a main, or backbone chain, of ethyleneand other insertion copolymerizable monomers, containing randomlydistributed side chains of ethylene and other insertion copolymerizablemonomers. The backbone chain has a weight-average molecular weight fromabout 5,000 to about 1,000,000 Daltons, preferably from about 10,000 toabout 500,000 Daltons, most preferably from about 20,000 to about200,000 Daltons. The side chains have weight-average molecular weightsfrom about 2,500 to about 125,000 Daltons, preferably from about 3,000to about 80,000 Daltons, most preferably from about 4,000 to about60,000 Daltons. As expressed in M_(e) ^(B), side chains haveweight-average molecular weights ranging from above 2 to 100 times theentanglement weight of copolymer, preferably 3-70 times the entanglementweight of copolymer, and most preferably 4-50 times the entanglementweight of copolymer. The number of side chains per backbone chain isdetermined by the average spacing between the branches, the backbonesegment between each branch averaging a weight average of at least twicethe entanglement molecular weight of polyethylene, preferably 3 to 25times the entanglement molecular weight of polyethylene. In practicethis establishes a number of arms of from 2-100, preferably 2-70, mostpreferably 3-50.

[0010] The MWD, defined as the ratio of weight-average molecular weightto number-average molecular weight, for both the backbone chain and thesidechains, independently, can be from 1.0-6, preferably 1-5, and mostpreferably 1-3.5.

Rheological Properties

[0011] Definition of linear viscoelastic behavior of polymeric materialsis complex, but utilizes well known concepts. Thus, the invention may bedescribed in terms of melt rheological parameters including theNewtonian limiting viscosity, the rubbery plateau modulus, and in termsof “shear thinning” characteristics readily quantified in terms of theratio of the Newtonian limiting viscosity (η₀) to the absolute value ofthe complex viscosity in oscillatory shear (η*) at 100 rad/sec at 190°C. Shear thinning may be characterized by the ratio of the Newtonianviscosity (η₀) to viscosity the complex viscosity at an arbitrarilychosen frequency of 100 rad/sec (η*₁₀₀). This η₀ may be measured invarious ways well known to those skilled in the art. Included amongthese are rotational oscillatory shear rheometry and totaional steadyshear rheometry, including shear creep. The value of η₀ may be obtainedfrom these methods by direct observation of the frequency independent orshear rate independent value of viscosity, or it may be determined froman appropriate fitting equation such as the Cross equation when the dataextend into the Newtonian region. Alternative data handling methodsincluded evaluating the limiting value of the ratio of the loss modulusto frequency, G″/ω, at low frequency:

η₀=lim G″/ω|_(ω→0),

[0012] or by linearly extrapolating the reciprocal of viscosity vs.shear stress to zero shear stress (e.g., G. V. Vmogradov, A- Ya. Maikin,Rheology of Polymers, Mir Publications Moscow, Springer-Verlag, p.153(1980)). Direct observation of the frequency independent value of thecomplex viscosity, η*, from rotational oscillatory shear and/or thefitting of the Cross equation to the same data were the methods used forthis description.

[0013] At low frequencies the melt viscosity expressed as the absolutevalue of the complex viscosity (η*) of high polymers is independent ofthe frequency, i.e., it is constant with frequency and is called theNewtonian limiting viscosity, η₀. At increasing frequencies η* decreaseswith increasing frequency in a manner determined by its relaxationspectrum and this decrease in viscosity is called shear thining (or,pseudoplasticity in earlier nomenclature). The plateau modulus may bedefined in several interrelated ways, e.g., the value of the storagemodulus (real part of the complex modulus), G′, in a region of G′constant with frequency, or the value of G′ at the frequency of aminimum in the loss modulus (imaginary part of the complex modulus), G″,or the value of G′ at the minimum in tan δ, where tan δ=G″/ G′, or otherdefinitions which lead to similar answers. For purposes of thedescription we chose to use the ratio of the Newtonian viscosity to thecomplex viscosity as discussed above.

[0014] Definitions and description of these and other parametersdiscussed here may be found, e.g., in Ferry (J. D. Ferry, ViscoelasticProperties of Polymers, 3rd Ed., John Wiley & Sons, N.Y., 1980) and inDealy and Wissbrun (J. M. Dealy, K F. Wissbrun, Melt Rheology and ItsRole in Plastics Processing. Theory and Applications, Van NostrandReinhold, N.Y., 1990). The methods of measurement, e.g., rotationaloscillatory shear between parallel circular plates in an instrument suchas a Rheometrics Scientific Mechanical Spectrometer, and data treatment,e.g., interconversion of complex variable Theological parameters andtime-temperature superposition, are also well known and frequently usedby those of ordinary skill in the art. Again, these are largelydescribed in the above references and in numerous other texts andpeer-reviewed publications in the field.

[0015] The ability of a polymer to exhibit strain hardening underextension (i.e., or increase of the extensional viscosity with strainrate) has been shown to correlate with the melt strength of that polymerand the ease of forming a bubble from it as in blown film operations inindustry. A measure of the strain hardening can be given as follows. Onecan predict what the extensional viscosity would be if the polymerobeyed linear viscoelasticity through the model of Chang and Lodge(Chang, H.; and Lodge, A- S.; Rheologica Acta, 11, pp. 127-129 (1972)).This is shown in the FIG. V as η_(ext),(linear). This can be compared tothe experimentally measured viscosity, called η_(ext) (measured) in thefigure. The sharp rise of next (measured) over the predicted valueη_(ext) (linear) is the result of strain hardening. To extract a numberfrom the data that expresses the degree of this strain hardening, weselected the value of η_(ext) (measured) at conditions characteristic offilm blowing—a strain rate of 1 secd⁻¹, temperature of 190° C., and timeof 3 sec. The ratio then becomes the measured value divided by thatpredicted by the Chang and Lodge model at the same temperature and time.This ratio must be greater than 2 for clear evidence of strainhardening, so it can be represented as the following:

η_(ext) (measured)/η_(ext)(linear)≡η_(ext)ratio≧2.

[0016] Polymer melt elongation (or extension) is another importantdeformation in polymer processing. It is the dominant deformation infilm blowing, blow molding, melt spinning, and in the biaxial stretchingof extruded sheets. Often, an extensional deformation producingmolecular orientations takes place immediately before solidificationresulting in anisotropy of the end-use properties. Extensional rheometrydata are very sensitive to the molecular structure of a polymer systemtherefore, these data is a valuable tool for polymer characterization.

[0017] The time dependent uniaxial extensional viscosity was measuredwith a Rheometrics Scientific Melt Elongational Rheometer (Row). The RMEis an elongational rheometer for high elongations of polymer melts. Thesample is supported by an inert gas, heated to the test temperature byelectrical heaters mounted in the side plates of the rheometer. Thetemperature is controlled from ambient to 350° C. The polymer meltsample is extended homogeneously by two metal belt clamps, eachconsisting of two metal belts with its fixtures. The metal belts controla range of extensional strain rates from 0.0001 to 1.0 s⁻¹. The forcesgenerated by the sample are measured by a spring type transducer with arange from 0.001 to 2.0 N. The maximum Hencky strain achievable by thisinstrument is 7 ( stretch ratio=1100). This instrument is based upon apublished design, see Meissner, J., and J. Hostettler, Rheological Acta,33, 1-21 (1994), and is available from Rheometrics Scientific, Inc.

[0018] The rheological behavior of these polymers with controlledbranching shows surprising and useful features. These polymers have azero-shear viscosity that is larger than a linear polymer of the samemolecular weight. They show a rapid drop in viscosity with shear rate(large degree of shear thinning); and a plateau modulus that is at leasttwo times lower than that of prior art linear and branched polymers.This latter characteristic is especially surprising, since ethylenepolymers of various types exhibit essentially the same plateau modulus.This was thought to be intrinsic to the monomer type and not dependenton polymer architecture. The lower plateau modulus means that the combpolymers likely are much less entangled than the linears, thus giving itsuch low viscosity for their molecular weight. The utility of theseproperties of the invention polymers is that they have a very lowviscosity for its molecular weights under melt processing conditions andso will process much more easily than the prior art polymers whileexhibiting increased extensional viscosity indicative of increased meltstrength.

Polymer Preparation

[0019] Initial studies conducted to determine optimum polymer structuressuitable for the improved properties sought were based on knowledge asto production of hydrocarbon polymers with precisely controlledstructures through the saturation of anionically synthesized polydienes.Various polydienes can be saturated to give structures that areidentical to polyolefins as was reported by Rachapudy, H.; Smith, G. G.;Raju, V. R.; Graessley, W. W.; J. Polym. Sci.—Phys. 1979, 17, 1211. Thetechniques completely saturate the polydiene without any side reactionsthat might degrade or crosslink the molecules. The controlled molecularweight and structure available from anionic polymerization of conjugateddienes are thus preserved. A unit of butadiene that has beenincorporated 1, 4 into the polybutadiene chain will have the structureof two ethylenes (four methylenes) after saturation, and those that goin as 1, 2 will be like one butene unit. So the saturated versions ofpolybutadienes of a range of microstructures are identical in structureto a series of ethylene-butene copolymers. Similarly saturatedpolyisoprenes resemble an alternating ethylene-propylene copolymer, andother polydienes can give the structures of polypropylene and otherpolyolefins upon saturation. A wide variety of saturated hydrocarbonpolymers can be made in this way.

[0020] Thus linear ethylene-butene copolymers can be made by thesaturation of linear polybutadienes and linear ethylene-propylenecopolymers of the invention can be made by the saturation of linearpolyisoprenes. The linear polymers can be prepared by anionic synthesison a vacuum line in accordance with the teachings of Morton, M.;Fetters, L. J.; Rubber Chem. & Technol. 1975, 48, 359. The polymers ofthe invention made in this manner were prepared in cyclohexane at −0°C., with butyllithium as initiator. The polydiene polymers were thensaturated under H₂ pressure using a Pd/CaCO₃ catalyst of J. Polym.Sci.—Phys. 1979, 17, 1211, above. This technique can be used to makepolymers over a wide range of molecular weights, e.g. polymers withmolecular weights from 3,500 to 800,000.

[0021] The branched polymers of the invention can be made by attachingone or more linear polymers, prepared as above, as branches to anotherof the linear polymers serving as a backbone or main chain polymer. Thegeneral method is to produce branch or arm linear polymers by theprocedure above, using the butyllithium initiator; this produces apolybutadiene with a lithium ion at the terminal end. A linear backboneis made in the manner described above, some number of the pendant vinyldouble bonds on the backbone polymers are then reacted with (CH₃)₂SiClHusing a platinum divinyl tetramethyl disiloxane catalyst. The lithiumends of the arm polybutadiene polymers then are reacted with theremaining chiorines on the backbone polybutadiene vinyls, attaching thearms. Because both the placement of the vinyl groups in the backbone andthe hydrosilylation reaction are random, so is the distribution of armsalong and among the backbone molecules. These polybutadiene combs can besaturated as shown above to form ethylene-butene copolymer combs withnearly monodisperse branches randomly placed on a nearly monodispersebackbone. Polymers having two branches can be made by a similarsynthetic procedure. Four anionically synthesized polymers (arms) areattached to the ends of a separately synthesized polymer (“connector”),two at each end. This results in an H-shaped structure, i.e., asymmetric placement of the arms and non-random distribution of the ofarms of the molecule.

[0022] An alternate method of preparing the branched olefin copolymersof the invention, particularly ethylene copolymers, is by preparingolefinically unsaturated macromers having molecular weight attributeswithin that described for the branch or arm polymers or copolymers andincorporating those into a branched polymer by copolymerization. Suchcan be done, for example, by preparing branch macromers from olefinssuch that there is vinyl or vinylidene unsaturation at or near themacromer chain end. Such is known in the art and the teachings of thebackground art as to the use of metallocenes to prepare these macromers,and then to insert or incorporate the macromers into a forming polymeras long chain branches, are applicable in this regard. Each of U.S. Pat.No. 5,324,800 and international publication WO 94/07930 are incorporatedby reference for purposes of U.S. patent practice. Such can beaccomplished by the use of series reactions or in situ single processeswhere the selection of catalyst or catalyst mix allows for thepreparation of olefinically unsaturated macromers and subsequentincorporation of them into forming polymeric chains.

[0023] In order to assure the quality and number of branches sought, itis suitable to use a multistep reaction process wherein one or morebranch macromers are prepared and subsequently introduced into areaction medium with a catalyst capable of coordination copolymerizationof both the macromer and other coordination polymerizable monomers. Themacromer preparation preferably is conducted so as to prepare narrow MWDmacromers, e.g., 2.0-3.5, or even lower when polymerization conditionsand catalyst selection permit. The comonomer distribution can be eithernarrow or broad, or the macromer can be a homopolymeric macromer. Theuse of essentially single site catalysts, such as metallocene catalysts,permits of the sought narrow MWD. Branch separation, or statedalternatively, branch numbers by molecular weight of the backbone chain,is typically controlled by assuring that the reactivity ratios of themacromers to the copolymerizable monomers is in a ratio that allows thepreferred ranges for the branch structure as described above. Such canbe determined empirically within the skill in the art. Factors to beadjusted include: catalyst selection, temperature, pressure, and time ofreaction, and reactant concentrations, all as is well-known in the art.

[0024] In this manner, branched copolymers are made directly withouthydrogenation and the selection of comonomers is extended to the fullextent allowed by insertion or coordination polymerization. Usefulcomonomers include ethylene, propylene, 1-butene, isobutylene, 1-hexene,1-octene, and higher alpha-olefins; styrene, cyclopentene, norbornene,and higher carbon number cyclic olefins; alkyl-substituted styrene or ;alkyl-substituted norbornene; ethylidene norbornene, vinyl norbornene,1,4-hexadiene, and other non-conjugated diolefins. Such monomers can behomopolymerized or copolymerized, with two or more copolymerizablemonomers, into either or both of the branch macromers or backbone chainsalong with the macromers. The teachings of co-pending U.S. provisionalpatent application Ser. No.60/037323 (Attorney Docket No. 96B006) filedFeb. 7, 1997, is incorporated by reference for purposes of U.S. patentpractice. See also the examples below where a mixed zirconocene catalystwas used in a fluidzed gas phase polymerization of an ethylene-hexenecopolymer product which contained component copolymer fractions meetingthe limiting elements of the invention described herein.

Industrial Applicability

[0025] The branched polyethylene copolymers according to the inventionwill have utility both as neat polymers and as a portion or fraction ofethylene copolymer blend compositions. As neat polymers, the polymershave utility as film polymers or as adhesive components, the discussionof WO 94/07930 being illustrative. The fabricated articles of U.S. Pat.Nos. 5,272,236 and 5,278,272 are additionally illustrative.

[0026] The copolymers of the invention will also have utility in blends,those blends comprising the branched copolymer of the invention at from0.1-99.9 wt. %, preferably from 0.3-50 wt. %, more preferably 0.5-25 wt.%, and even more preferably 1.0-5 wt %, the remainder comprising anessentially linear ethylene copolymer of weight-average molecular weightfrom about 25,000 Daltons to about 500,000 Daltons, typically thosehaving an MWD of from about 1.75-30, preferably 1.75-8.0, and morepreferably 1.9-4.0, with densities form 0.85 to 0.96, preferably 0.85 to0.93, as exemplified by the commercial polymers used for comparison inthis application. The blends in accordance with the invention mayadditionally comprise conventional additives or adjuvants inconventional amounts for conventional purposes. The blends according tothe invention exhibit improved processing, largely due to the inclusionof the branched ethylene copolymer according to the invention, and canbe more easily processed in conventional equipment.

EXAMPLES Example 1—Preparation of C1

[0027] A comb polybutadiene polymer (PBd) was prepared by couplinghydrosilylated polybutadiene backbone chains with polybutadienyllithiumsidechains, or branches. The polybutadiene which was used as backbonefor the hydrosilylation reaction was prepared by anionic polymerizationusing high vacuum techniques, with sec-BuLi in benzene at roomtemperature. (Characterization=M_(n)106,500 by size exclusionchromatography (SEC) based upon a polybutadiene standard; 10% 1,2units). 10 grams of this backbone polymer chain were dissolved in 120 mltetrahydrofuran (THF) in an one-liter round bottom flask equipped with agood condenser, to which 3 drops of platinum divinyl tetramethyldisiloxane complex in xylene (catalyst, Petrarch PC072) were added. Thesolution was dried overnight with 1.5 ml trimethylchworosilane, followedby the addition of 7.55 mmole dimethylchworosilane. The mixture'stemperature was raised slowly to 70° C. Changing of the color, vigorousboiling and refluxing indicated the start of the reaction which wascontinued for 24 hours at 70° C. THF and chlorosilane compounds wereremoved in the vacuum line by heating the polymer at 45° C for 5 days.The hydrosilylated polymer was freeze dried under high vacuum for 2days.

[0028] Living polybutadiene branch polymers (PBdLi, M_(n)=6,400 by SEC;T3) used for the coupling reaction was prepared in the same manner asthe backbone. The synthesis of PBdLi was performed by reacting 12.75grams of butadiene monomer with 2.550 mmoles of initiator. Prior to thecoupling reaction 1 gram of PBdLi was removed, terminated with methanoland used for characterization. 40% excess of PBdLi was used for thecoupling reaction, which was monitored by SEC and allowed to proceed for2 weeks. Excess PBdLi was terminated with methanol. The comb polymer wasprotected against oxidation by 2,6-di-tert-butyl-p-cresol and wasfractionated in a toluene-methanol system. Fractionation was performeduntil no arm or undesirable products were shown to be present by SEC.The comb was finally precipitated in methanol containing antioxidant,dried and stored under vacuum in the dark. Characterization, which wascarried out by SEC, membrane osmometry (MO), vapor pressure osmometry(VPO), low-angle laser light scattering (LALLS), and laser differentialrefractometry, indicated the high degree of molecular and compositionalhomogeneity. Molecular characterization results are shown in Table I.Using the M_(n) (MO, VPO) and M_(w) (LALLS) of Table I the number ofarms experimentally obtained is calculated, which is smaller than thetheoretically expected, indicating a small yield in the hydrosilylationreaction. Fractionation and characterization results are shown in TableI and II.

[0029] The number of branches, or sidechains, was determined by both¹³C-NMR and ¹H-NMR. Resonances characteristic of methyl groups adjacentto a Si atom (at the point of connection to the backbone) was found fromboth methods: similarly, resonances characteristic of the methyladjacent of the methine in a sec-butyl group (at the terminus of the armfrom the initiator used to polymerize it) was measured. From thecombination of these methods, the number of arms per 10,000 carbons wasfound to be 15+5, which is consistent with 34 arms for this example.

[0030] The resulting comb (branched polybutadiene polymer) (“C1”) wassaturated catalytically. 3 grams of the comb polymer were dissolved incyclohexane and reacted with H₂ gas at 90° C. and 700 psi in thepresence of 3 g of a catalyst made by supporting Pd on CaCO3. Thereaction was allowed to proceed until the H₂ pressure stopped dropping,or about 24 h. The polymer solution was then filtered to remove thecatalyst residues. The saturation of the polymer was seen to be greaterthan 99.5% by proton NMR. The polymer was thus converted byhydrogenation to an ethylene-butene branched copolymer. See Tables I andII, below.

Example 2—Preparation of C2

[0031] 8 grams of PBd (M_(n)=87,000 by MO, prepared as described inExample 1; BB₃) dissolved in 150 ml THF were hydrosilylated in the samemanner as described in Example 1, using 0.5 ml of trimethylchiorosilaneand 2.43 mmoles of dimethylchlorosilane. The hydrosilylated polymer wasfreeze dried under high vacuum for 5 days. PBdLi (M, =4,500 by VPO; T₅)was prepared as described in Example 1 by reacting 11.5 grams ofbutadiene with 2.550 mmoles of initiator. 1 gram of T₅ was removed inorder to be used for characterization purposes. The coupling reactionwas accomplished as described in Example 1. Fractionation andcharacterization results are shown in Table I and Table II.

[0032] The resulting comb PBd (C2) was saturated catalytically as inExample 3. The saturation of the polymer was seen to be greater than99.5% by proton NMR. The resulting saturated polymer had an M_(w) of97,000 by LALLS.

Example 3—Preparation of C3

[0033] 2 grams of PBd (M_(n)=108,000 by SEC, prepared as described inExample 1; BB4) dissolved in 50 ml THF were hydrosilylated in the samemanner as described in Example 1, using 0.5 ml of trimethylchlorosilaneand 0.77 mmoles of dimethylchiorosilane. The hydrosilylated polymer wasfreeze dried under high vacuum for 2 days. PBdLi (M_(n)=23,000 by SEC;T6) was prepared as described in Example 1 by reacting 22 grams ofbutadiene with 0.936 mmoles of initiator. 1 gram of T6 was removed inorder to be used for characterization purposes. The coupling reactionwas accomplished as described in Example 2. Fractionation andcharacterization results are shown in Table I and Table II.

[0034] The resulting comb PBd (C3) was saturated catalytically as inExample 3. The saturation of the polymer was seen to be greater than99.5% by proton NMR. The resulting saturated polymer had an M_(w) of598,000 by LALLS.

Example 4—Preparation of C4

[0035] 6 grams of PBd (M_(n)=100,000 by SEC, prepared as described inExample 1; BB5) dissolved in 60 ml THF were hydrosilylated in the samemanner as described in Example 1, using 1.0 ml of trimethylchlorosilaneand 3.83 mmoles of dimethylchlorosilane. The hydrosilylated polymer wasfreeze dried under high vacuum for 2 days. PBdLi (M_(n)=5,100 by SEC;T7) was prepared as described in Example 1 by reacting 27 grams ofbutadiene with 5.370 mmoles of initiator. 1 gram of T7 was removed inorder to be used for characterization purposes. The coupling reactionwas accomplished as described in Example 2. Fractionation andcharacterization results are shown in Table I and Table II. Theresulting comb PBd (C4) was saturated catalytically as in Example 3. Thesaturation of the polymer was seen to be greater than 99.5% by protonNMR. TABLE I Molecular characteristics of precursors and final polymers.10⁻³ M_(n) 10⁻³ M_(n) 10⁻³ M_(w) 10⁻³ M_(w) Part Sample (SEC)^(a)(MO)^(b) (LALLS)^(c) (VpO)^(d) M_(w)/M_(n) Backbone BB₂   106.5 101 103— 1.05 Arm T₃    6.4 — — 6.5 1.03 Comb Cl 274 — — 1.07 Backbone BB₃  99.0  87   90.0 — 1.04 Arm T₅    4.8 — — 4.5 1.05 Comb C2 —   105.5107 1.08 Backbone BB₄ 108  97 104 1.05 Arm T₆  23   23.5 1.04 Comb C3 —612 1.07 Backbone BB₅ 100   100.5 — — 1.04 Arm T₇  51 — —  4.75 1.04Comb C4 — 194 198 — 1.04

[0036] TABLE II Number of arms Comb Maximum possible^(a) Calculated^(b)Measured^(d) Yield (%) C1 100 29^(c) 34 29-34 C2 —   3.9  2.4 — C3 —22^(c) — — C4 — 19^(c) — —

Example 5—Preparation of Blend 1

[0037] Blend 1:6.8685 g of EXCEED(® 103 (“ECD103”), a commerciallyavailable ethylene-l-hexene linear low density polyethylene of ExxonChemical Co. having a density of 0.917 and MI of 1.0, and 0.1405 g of C1(above) were dissolved in 100 ml of xylene at 130° C. 0.0249 g of astabilizer package (a 1:2 mixture of Irganox® 1076 and Irgafos®168 fromCiba-Geigy, Inc.) was also added. The solution was allowed to mix for 2hours at 130 ° C., and then the polymer blend was precipitated by addingthe xylene solution to 1800 ml of methanol chilled to 2 ° C. Theprecipitate was washed with more methanol, and the remaining xylene wasremoved by drying in a vacuum oven at 88 ° C for two days.

Example 6—Preparation of Blend 2

[0038] Blend 2 : 6.8607 g of the EXCEED® 103 (ECD103), 0.1402 g of C3(above) and 0.0248 of the stabilizer package were mixed in the samemanner as Blend 1.

H-shaped Polymer Examples Example 7—Preparation of HI Preparation ofArms

[0039] 6.3 ml (5.0 g) 1,3-butadiene was diluted in 75 ml benzene (6.1%w/v). To this solution was added 16.3 ml sec-BuLi 0.062M in n-hexane(1.01×10⁻³ mol sec-BuLi). After 24 h at room temperature the reactionwas complete. 1.0 g of the product polybutadiene (Y; M_(n)=5,500 by SEC)in 18 ml solution was removed for the characterization procedure and therest of Y was mixed with 8.3 ml CH₃SiCl₃ 0.046 M in benzene (0.38×10⁻⁴mol CH₃SiCl₃). After 7 days at room temperature the reaction wascomplete and the Y₂Si(CH₃)Cl was formed.

Preparation of Connector

[0040] A difunctional initiator was prepared by the addition ofsec-butyl lithium to 1,3-bis(1-phenyl ethenyl) benzene, resulting in1,3-bis(1-phenyl -3 methyl pentyl lithium) benzene, called here DLI.15.4 ml (11.4 g) 1,3-butadiene was diluted in 355 ml benzene (2.3% w/v).To this solution was added 33.8 ml of DLI 0.0225M in benzene (7.3×10⁻⁴mol DLI) and 8.4 ml of sec-BuLi 0.10M in benzene (8.36×10⁻⁴ molsec-BuLi). After 4 days at room temperature the reaction was complete.1.0 g of the product difunctional polybutadiene (X; M_(n)=27,100 by SEC;M_(w)=24,500 by LALLS) in 35 ml solution was removed for thecharacterization procedure. 4.8 g of X in 175 ml solution was removedfor the formation of the Y₂Si(CH₃)X(CH₃)SiY₂.

Formation of H1

[0041] 4.0 g of Y₂Si(CH3)Cl and 34.8 g of X were mixed. To the solutionwas added 1.0 ml THF. After 7 days at room temperature the formation ofthe Hi was complete. H1 comprised a structure having a backbone of about38,000 M_(n) plus tow Y arms and two brancheds each of about 5,500 Mn (Yarms).

Fractionation

[0042] The product of the previous reaction was precipitated in 1000 mlmethanol and was redissolved in 900 ml toluene (1% w/v). 450 ml methanolwas added and the solution was stirred at room temperature to reach thecloud-point. After that 20 more ml of methanol were added and thetemperature was increased slowly, until the solution became clear. Thenit was left to cool down and next day the separated part of the H1 wascollected, as the lower phase in a two-phase system. To the upper phasewas added 25 ml methanol, to reach again the cloud-point and then 20 mlmore methanol. The temperature was increased slowly and after theclearance of the solution, it was left to cool down. The newly separatedpart of the Hi was mixed with the previous part from the firstfractionation and it composed the final pure H1. By LALLS the H1 had anM_(w) of 50,000.

Saturation

[0043] The H1 was saturated in the same manner as in Example 3, exceptthat 0.2 g of triphenyl phosphate and 0.0366 g of tris(triphenylphosphine)rhodium(I)chloride were added to the reaction for every gramof polymer. Essentially complete saturation was achieved. The resultingsaturated polymer had an Mw of 48,000 by LALLS.

Example 8—Preparation of H2 Preparation of Arms

[0044] 9.0 ml (6.7 g) 1,3-butadiene was diluted in 65 ml benzene (10.3%w/v). To this solution was added 10.7 ml sec-BuLi 0.062M in n-hexane(6.66×10⁻⁴ mol sec-BuLi). After 24 h at room temperature the reactionwas complete. 1.0 g of the product polybutadiene (Z; M_(n)=11,000 bySEC; M_(w)=10,800 by LALLS) in 13 ml solution was removed for thecharacterization procedure and the rest of Z was mixed with 5.8 ml ofCH3SiCl_(3 0.046)M in benzene (0.27×10⁻³ mol CH₃SiCl₃). After 7 days atroom temperature the reaction was complete and the Z₂Si(CH₃)Cl wasformed.

Preparation of Connector

[0045] 3.4 g of X in 125 ml solution was removed for the formation ofthe Z₂Si(CH₃)X(CH₃)SiZ₂ (H2) in the manner of Example 7.

Formation of H2

[0046]5.7 g of Z2Si(CH₃)Cl and 3.4 g of X were mixed. To the solutionwas added 1.0 ml ThF. After 7 days at room temperature the formation ofthe H2 was complete. H2 had a resulting H-shaped structure like H1.

Fractionation

[0047] The procedure followed was the same as in Example 7. Theresulting polymer had an M_(w) of 67,000 by LALLS.

Hydrogenation

[0048] The procedure followed was the same as in Example 7. Theresulting saturated polymer had an M_(w) of 64,700 by LALLS.

Rheological Properties of Examples

[0049] The melt shear rheological behavior of the various resultingcopolymer examples was measured by well known methodology, i.e.,rotational sinusoidal oscillatory shear between parallel plates in aRheometrics Scientific RMS-800 Mechanical Spectrometer. Frequency rangesof from 0.1 to 100 rad/sec or from 0.1 to ca. 250 rad/sec or from 0.1 toca. 400 rad/sec or from 0.01 to 100 rad/sec or from 100 to 0.01 rad/secwere covered at a sequence of temperatures ranging from 120° C. to 250°C. and in some cases to as high as 330° C. Typically, the examples weretested at isothermal conditions from 0.1 to 100 rad/sec or to ca. 250rad/sec at 120° C., 150° C., 170° C., 190° C., and 220° C.,successively, and then from 0.01 to 100 rad/sec at 250° C., 280° C. orhigher as necessary to access the terminal linear viscoelastic regime.Repeat testing was periodically performed on the same specimens at 150°C. (sometimes at 220° C.) to check reproducibility. All measurementswere performed at strains within the linear viscoelastic regime, andeither one or two specimens were used to cover all temperatures tested.The parallel plates were 25mm in diameter and the gap between the plates(sample thickness) was precisely set at values from ca. 1.6 mm to 2.3 mmfor different test specimens and temperatures. Use of successivetemperature testing on single specimens requires compensation fortooling expansion with increasing set temperature in order to maintainconstant gap distance at all temperatures. This was accomplished in allcases by raising the upper platen (plate) at each new increasedtemperature by the amount 0.0029 mm/° C. Additionally, in some casessample expansion evidenced by normal stress increase was compensated bymaintaining a constant (low) normal stress in the sample at the varioustemperatures. The above methods are all well known to practicingrheologists. All samples were stabilized by addition of 1%(wt) of a 1:2mixture of Irganox® 1076/Irgafos®D 168 (Ciba-Geigy, Inc.) prior tocompression molding test specimens in a Carver Laboratory Press.

[0050] The resultant linear viscoelastic data, which may be expressed innumerous ways, but here were expressed as complex viscosity, η*, elasticstorage modulus, G′, loss modulus, G″, and complex modulus, G*, werethen superimposed to the 190° C. reference temperature by well knowntime-temperature superposition methodology, yielding master curves ofthe above parameters vs. frequency over up to seven orders of magnitudeof frequency from the terminal regime through the rubbery plateau region(where possible). Superposition specifically was performed by verticalshifting of the log₁₀ complex modulus according to the equation

b_(T)=ρ_(o)T_(o)/ρT

[0051] where b_(T) is the vertical shift factor, ρ is the melt densityat temperature, T's are absolute temperatures in OK, and the subscript,o, refers to the 190° C. reference temperature. Vertical shifting wasfollowed by arbitrary horizontal shifting of log₁₀ complex modulus alongthe log₁₀ frequency axis to yield the horizontal shift factors, a_(T),which were then fitted to an Arrhenius form equation to yield the energyof activation for viscous flow, E_(a), where E_(a) is derived from

a_(T)exp[(E_(a)/R)(1/T−1/T_(o))]

[0052] and where R=1.987×10⁻³ in kcal/mol ° K.

[0053] The following critical melt shear Theological attributes at 190°C., derived from the master curve data, describing aspects of theinvention are given in Tables III and VI for each of the examples:

[0054] Newtonian viscosity, η_(o), in Pa-s

[0055] Plateau modulus, G_(N) ^(o), in Pa (evaluated at the frequency ofG″minimum)

[0056] Ratio of Newtonian value to viscosity at 100 rad/sec,η_(o)/η*_((100s) ^(−1),)

[0057] Ratio of the extensional viscosity measured at a strain rate of 1sec⁻⁷, 190° C., and time=3 sec (i.e., a strain of 3) to that predictedby linear viscoelasticity at the same temperature and time, and

[0058] Energy of activation, E_(a).

[0059] The high Newtonian viscosities of the invention indicateadvantageously high extensional viscosities (at low strain rate). Thelow plateau moduli of the invention, as well as the measures of shearthinning, are indicative of low viscosity at, e.g., extrusion, blowmolding, and injection molding shear rates.

EXAMPLE 1-1 (C1)

[0060] C1 was ground into coarse powder and dry mixed with 1%(wt) of a1:2 mixture of Irganox® 1076/Irgafos® 168 (Ciba-Geigy, Inc.). Thismaterial was then compression molded into 1 inch (25.4 mm) diameter×2 mmthickness disks in a Carver Laboratory Press (Fred S. Carver, Inc.)using a cavity of these dimensions and Teflon® coated aluminum sheetliners. Molding was performed at ca. 190° C. and 10,000 psi. The meltlinear viscoelastic testing as a function of frequency was performed atthe various temperatures given below on two such specimens in aRheometrics Scientific RMS-800 Mechanical Spectrometer in parallel platesinusoidal oscillatory shear mode. Plate diameters and specimendiameters at test conditions were 25 mm and gap setting (samplethickness) at the initial 150° C was 1.865 mm. Measurements were made ona single specimen at 150° C. (0.1-251 rad/sec, 1.865 mm gap), 120° C.(0.1-251 rad/sec, 1.865 mm gap), 170° C. (0.1-251 radi/sec, 1.908 mmgap), 190° C. (0.1-158 rad/sec, 1.993 mm gap), and 220° C. (0.1-251rad/sec, 2.071 mm gap). On a second specimen, measurements were thenperformed at 220° C. (0.1-251 rad/sec, 2.081 mm gap), 250° C. (0.01-100rad/sec, 2.111 mm gap), and 220° C. (100-0.01 rad/sec, 2.081 mm gap).Maintaining the gap setting constant with increasing temperature at thelower temperatures was accomplished compensating for tooling thermalexpansion/contraction as described in the general section above. Theincreased gap setting at higher temperatures compensated both fortooling dimension change and for sample expansion, where the latter wasaccomplished by maintaining a constant (low) normal stress on thesample.

[0061] The resultant melt rheological parametric data were expressed asdescribed in the general section above and were superimposed to 190° C.reference temperature master curves covering seven decades of reducedfrequency in the well known manner described above using IRIS computersoftware (HIS version 2.5, IRIS Development, Amherst, Mass.). Specificvalues of the parameters, Newtonian viscosity, plateau modulus, ratio ofthe Newtonian viscosity to the viscosity at 100 rad/sec, and energy ofactivation for viscous flow, are given in Table III.

[0062] FIGS. I-IV illustrate the surprising features of the C1 ascompared to those of commercial low density and linear low densitypolyethylene polymers. G28

[0063] FIG. I shows that the invention C1 exhibited a stronger-frequencydependence of the viscosity than any of the comparative examples A, B,C, and D. This translates into lower energy input per throughput unitfor the invention polymer. Note, this plot is dependent on thetemperature and molecular weight of the example polymers, in addition toMWD and molecular architecture.

[0064] FIG. II is a plot of these variables in a reduced variable mannerthat renders viscosity curves which are independent of the temperatureand the magnitude of the molecular weight, hence the comparison was madeon equal footing. The differences were only due to the MWD and thebranching characteristics. Note that the reduced viscosities of the twoLDPE examples (A & B) were on top of each other. As for FIG. I, thisplot clearly shows that for high throughputs, as desired in meltprocessing, the invention Example I exhibited lower values of theviscosity than any of the comparative examples (A, B, C, & D). Thistranslates into lower energy requirements per throughput unit.

[0065] FIG. H1 shows that C1 exhibited a region over which G′ wasessentially frequency independent, which can be taken as the plateaumodulus. The behavior of the storage modulus of the comparative examplesshowed each to increase with the frequency, even after the frequency atwhich the invention reached a plateau. As with FIG. I the effects of themolecular weight and temperature have not been removed.

[0066] FIG. IV shows the storage modulus of the example polymers againstthe product of the zero shear viscosity and frequency, thus removing theeffects of temperature and molecular weight. Accordingly this plotreflects only the influence of the MWD and branching characteristics onthe behavior of the storage modulus. This plot unquestionably shows thatthe storage modulus of Example I reached the rubbery plateau regionwhereas the storage moduli of the comparative examples were stillincreasing with frequency.

EXAMPLE 2-1 (C2)

[0067] A single test specimen of C2 was prepared with stabilization andcompression molding as described in the general discussion above andtested at the sequence of temperatures, 150° C. (0.1-100 rad/sec, 1.221mm gap) 1200C (0.1-100 rad/sec, 1.221 mm gap), 170° C. (0.1-100 rad/sec,1.221 mm gap), 1900C (100-0.01 rad/sec, 1.221 mm gap), 220° C. (100-0.01rad/sec, 1.221 mm gap), and 150° C. (0.1-100 rad/sec, 1.221 mm gap). Theresultant melt Theological parametric data were expressed as describedin the general section above and were superimposed to 190° C. referencetemperature master curves covering six to seven decades of reducedfrequency in the well known manner described above using IRIS computersoftware (IRIS version 2.5, IRIS Development, Amherst, Mass.). Specificvalues of the parameters, Newtonian viscosity, plateau modulus, ratio ofthe Newtonian viscosity to the viscosity at 100 rad/sec, and energy ofactivation for viscous flow, are given in Table III.

EXAMPLE 3-1 (C3)

[0068] A single test specimen of C3 prepared as in Example 2-1 wastested at a sequence of temperatures ranging from 120° C. to 330° C.with repeat tests at 1500C performed after the 250° C. and the 300° C.tests. The frequency ranges at the individual temperatures were asdescribed in the general description of methodology above. The resultantmelt rheological parametric data were expressed as described in thegeneral section above and were superimposed to 190° C. referencetemperature master curves covering seven to eight decades of reducedfrequency by the methods described in Examples 1-1 and 2.-1 Specificvalues of the parameters, Newtonian viscosity, plateau modulus, ratio ofthe Newtonian viscosity to the viscosity at 100 rad/sec, and energy ofactivation for viscous flow, are given in Table III.

EXAMPLES 4-1 through 8-1 (C4, BLEND 1, BLEND 2, H1, H2)

[0069] Examples 4-1 through 8-1 were prepared and tested variouslywithin the general methodology described in the above sections. The datafrom the various temperatures for each example were superimposed to1900C master curves as described in Example 1-1. Specific values of theparameters, Newtonian viscosity, plateau modulus, ratio of the Newtonianviscosity to the viscosity at 100 rad/sec, and energy of activation forviscous flow, are given in Table III. Where specific values are omitted,they could not be determined with reasonable certainty from the data.

EXAMPLE 9-1 (ECD103) (Comparative)

[0070] Example 9-1 was linear polyethylene used in the blends, Examples5-1 and 6-1. It was stabilized as described in the general methoddescription and compression molded into a 2.5in.×2.5in.×2 mm plaque fromwhich three 25 mm diameter×2 mm thickness disks were cut. Meltviscoelastic testing was performed on the first specimen from 0.1 to 400rad/sec at the succession of temperatures, 130° C., 120° C., 1150C, 150°C. Subsequently tests were performed on separate specimens from 0.1 to100 rad/sec at 170° C. and at 190° C. Data superposition to 190° C.master curves was performed as described in previous examples, andspecific values of the parameters, Newtonian viscosity, plateau modulus,ratio of the Newtonian viscosity to the viscosity at 100 rad/sec, andenergy of activation for viscous flow, are given in Table III. Wherespecific values are omitted, they could not be determined withreasonable certainty from the data.

Sample Preparation For Extensional Rheology

[0071] Samples identified in Tables III and VI were tested in aRheometrics Polymer Melt Elongational Rheometer (RME) for the value ofthe η_(ext) ratio. They prepared as rectangular parallelepipeds whoselength, width and thickness are approximately 60, 8, and 1.5 mm,respectively. These samples were prepared by compression molding thepolymer of interest within a brass mask.

[0072] The first step in the procedure used to mold these samples was toweigh out approximately 0.9 g of polymer, which was sufficient tocompletely fill the mask. When the bulk material was in pellet or powderform, the weighing process was straightforward. However, when thematerial to be tested was received in hard chunks, an Exacto knife wasused to cut small pieces of polymer from the bulk until theaforementioned mass had been collected. The next step was to stabilizethe polymer, which was only necessary for those materials that were notin pelletized form. This was accomplished by adding one weight percentIRGAFOS® 168 stabilizer (Ciba-Geigy, Inc.) to the weighed out polymer.The brass extrusion die was then filled with the stabilized polymer, andsandwiched between heated platens at 190° C. that are mounted on ahydraulic press (Carver Inc.) The purpose of the die is to mix themelted polymer so that the resulting test specimens are free of airbubbles and weld lines. The presence of either can cause the testspecimen to break at lower total strains versus the case in which thepolymer chains of the test specimen are fully entangled. Note that1″×1″×{fraction (1/16)}″ sheets of mylar were used to cap the die inorder to keep the polymer within the die from contacting and sticking tothe platens.

[0073] Once the polymer had melted within the die, the bottom sheet ofmylar was removed, and the plunger was placed into the hole of the die.The brass mask was then mounted onto the bottom platen, with a sheet ofmylar (3″×2″×{fraction (1/16)}″) being placed between the mask and theplaten. The die and plunger were then placed onto the brass mask, sothat the hole of the die coincided with the geometric center of the maskslit. The polymer was then extruded into the mask by closing the platensof the press, which drove the plunger into the die. The mask and diewere then removed from the press and allowed to cool to approximately100° C. at which point the mask was separated from the die. Because thesample held within the mask is not dimensionally homogeneous afterextrusion, it was remolded within the press at 190° C. and 2000 psibetween two 4″×2″×{fraction (1/16)}″ mylar sheets. After applying heatto the sample and mask for approximately ten minutes, the power to theplaten heaters was turned off, and the sample and mask were allowed tocool to room temperature (approximately 2 hours). It was necessary toslowly cool the polymer specimen in this way so that the molded samplewas free of residual stresses. Finally, the specimen was carefullyremoved from the mask. its dimensions were measured, and it was testedwithin the RME. Sample Testing in the Rheometrics Polymer MeltElongational Rheometer (RME) After allowing for the oven of the RME toheat up to the desired testing temperature, calibration of the forcetransducer was performed. This was accomplished with the rotary clamps(with stainless steel belts) installed, and the top clamp on thetransducer side (right-hand side) of the oven in the lowered position.With no mass hanging from the transducer shaft and pulley located at theback of the oven, the force calibration window was brought up in thedata acquisition software. After choosing the desired force scale, theforce gain was set to unity, and offset values were input until theaverage force readout on the screen was zero. A mass corresponding tothat chosen for the force scale was then attached to the transducershaft and hung over the pulley. The gain in the calibration window wasthen adjusted until the average measured force was equal to the massattached to the transducer. Once this was accomplished, the mass wasremoved from the shaft/pulley and the offset in the force calibrationwindow was adjusted until me average measured force. was again zero. Themass was then re-attached and the gain was readjusted until the properforce readout was achieved. This procedure of zeroing and scaling thetransducer readout was repeated iteratively until values for the offsetand gain in the calibration window of the data acquisition software wereobtained that simultaneously yielded a zero force when the transducershaft was load free and the proper force for the attached mass.

[0074] After calibrating the force transducer and measuring thedimensions of the parallelepiped test specimen, the temperature withinthe oven was checked to ensure that the oven was at the appropriate testtemperature. The valve on the gas flow regulator was then turned 180° sothat 99.6% pure nitrogen was delivered to the oven for temperaturecontrol. After waiting for the oven to be flooded with nitrogen gas (2-3minutes), the specimen was loaded between the rotary clamps using theRME loading block (i.e. the top clamps are in locked or upper position).Typically, 16 (cm³/min) of gas were delivered to the air table, while 14(cm³/min) were used to heat the rotary clamps. During loading it wasimportant for the specimen not to touch the top of the air table,because this can cause the specimen to stick and an extra force will bemeasured during elongational testing.

[0075] Immediately after releasing the specimen above the air table, theright-hand clamp was lowered to hold the specimen in place The samplewas then allowed to melt, while being levitated over the table forapproximately 5-6 minutes. The left-hand rotary clamp was then closed,and the specimen was checked to insure that it did not stick to the airtable. Generally, the melted specimen had sagged somewhat between thetable and the clamps, which can cause some sticking to the air table anderroneous force data at low strains. To overcome this problem, the slackwas drawn up by jogging the clamps at an angular velocity of 1 rev/min.Sample testing was then initiated by setting the VCR to record mode,initiating the video timer, and choosing start test in the dataacquisition software, respectively. Subsequent to the sample beingelongated, the valve on the gas flow regulator was returned to the airside, and the required test parameters were entered into the dataacquisition software. The rotary clamps and oven door were then opened,and the clamps were removed. Finally, the tested polymer was extractedfrom the stainless steel belts, and recycled for additional elongationaltests. TABLE III 190° C. SHEAR RHEOLOGY and EXTENSIONAL RHEOLOGYEXAMPLES η₀ (190° C.) Linear η₀ Equivalent G_(N) ⁰ η₀/η* E_(a) EXAMPLE(Pa · s) (Pa · s) (Pa) η_(ext) ratio (100s⁻¹) (kcal/mol) MULTIPLYBRANCHED (>2) STRUCTURES 1 (C1) 1.0 × 10⁶ 1.0 × 10⁵ 1.3 × 10⁵ — 710   18.4 2 (C2)   9 × 10⁵ 4.5 × 10³  ˜6 × 10⁵ — 130    15.0 3 (C3)  >5 × 10⁷1.6 × 10⁶  ˜3 × 10⁴ — >1200     17.6 4 (C4)  >1 × 10⁷ 3.5 × 10⁴  ˜3 ×10⁵ — >2500     17.0 (No terminal region) 5 (BLEND 1) 7.5 × 10³ — — 2.253.2  7.88 (2% C1/98%ECD103) (Rubbery plateau not accessed) 6 (BLEND 2)  8 × 10³ — — 3.18 3.3  8.54 (2% C3/98%EDC103) (Rubbery plateau notaccessed) H-STRUCTURES 7 (H1) 6.4 × 10³ 3.0 × 10²   5 × 10⁵ — 2.4 12.2 8(H2) 6.4 × 10⁴ 8.2 × 10²  ˜3 × 10⁵ — 26   15.8 LINEAR 9 (ECD103)(Comparative) 6.7 × 10³ 8.3 × 10³ — 1.48 2.7  7.86

Example 10—In situ Mixed Zirconocene Catalyst Example

[0076] This example illustrates the preparation of branched copolymersvia an in situ coordination polymerization method using a mixedzirconocene catalyst as described in U.S. Pat. No 5,470,811.

[0077] 1) Preparation of mixture of isomers of (MeEtCp)₂ZrCl₂[bis(1,2-MeEtCp)ZrCl₂, bis(1,3-MeEtCp)ZrCl₂, and (1,2-MeEtCp)(1,3-MeEtCp)ZrCl₂, where Me =methyl, Et=ethyl, Cp=cyclopentadienyl],hereinafter called (1,2/1,3-MeEtCp)₂ZrCl₂:

[0078] Methylcyclopentadiene dimer was cracked to the monomeric unitsover high viscosity silicone oil. A sample of the freshly preparedmethylcyclopentadiene (100.5 g, 1.26 mol) was diluted in 500 cm³tetrahydrofuran in a 3-liter flask. The flask was cooled in an ice-bathto 0° C. and 900 cm³ of 1.4 M solution of methyllithium in hexane wasadded slowly. After complete addition of the MeLi the ice-bath wasremoved and stirring continued for 3 hours at room temperature. Then theflask was cooled again to 0° C. and bromoethane (139.2 g, 1.28 mol) wasadded slowly as solution in THF. The mixture was then stirred for 15hours. The resulting product was washed with distilled water and theorganic layer was dried over sodium sulfate.

[0079] This was then filtered and concentrated under vacuum and theconcentrate was dissolved with a gentle N₂ sparge. The fraction boilingbetween 118-120° C. was saved.

[0080] Freshly distilled methylethyl-cyclopentadiene isomers (41.9 g,0.388 mol) as above was dissolved in 30 cm³ THF. 242 cm³ of 1.6 Msolution of n-BuLi in hexane was slowly added to this and stirring wascontinued for 3 hours after all the n-BuLi had been added. This solutionwas then added slowly to a slurry of ZrCI4 (45.2 g; 0.194 mol.) in 200cm³ THF at −80° C. Stirring continued for 15 hours as the temperatureslowly warmed up to 20° C. The solvent was removed under vacuum and thesolid recovered was extracted with toluene. The toluene extract wasconcentrated and pentane was added to aid precipitation of the purecompound at −30° C.

[0081] 2.) Preparation of Mixed Zirconocene Catalyst:

[0082] 2300 g of Davison 948 silica dried at 200° C. was slurried in6000 cm³ heptane in a reaction flask. The flask was maintained at 24° C.and 2500 cm³ of 30 wt % methylalumoxane in toluene was added. After 0.5hours, the temperature was raised to 68° C., and maintained for 4 hours.Then a toluene solution of 24.88 g (1,3-MeBuCp)₂ZrCI₂ (where Bu isbutyl), mixed with 21.64 g of the isomeric mix (1,2/1,3-MeEtCp)₂ZrCl₂,prepared above, was added slowly followed by a 1 hour hold of thereaction conditions. Then the resultant catalyst was washed with hexane4 times and then dried to a free-flowing powder with a gentle N₂ flow.

Fluidized-Bed Polymerization

[0083] The polymerization was conducted in a continuous gas phasefluidized bed reactor. The fluidized bed was made up of polymergranules. The gaseous feed streams of ethylene and hydrogen togetherwith liquid comonomer were mixed together in a mixing tee arrangementand introduced below the reactor bed into the recycle gas line. Hexenewas used as comonomer. Triethyl aluminum (TEAL) was mixed with thisstream as a 1% by weight solution in isopentane carrier solvent. Theindividual flow rates of ethylene, hydrogen and comonomer werecontrolled to maintain fixed composition targets. The ethyleneconcentration was controlled to maintain a constant ethylene partialpressure. The hydrogen was controlled to maintain a constant hydrogen toethylene mole ratio. The concentration of all the gases were measured byan on-line gas chromatograph to ensure relatively constant compositionin the recycle gas stream.

[0084] The solid catalyst (above) was injected directly into thefluidized bed using purified nitrogen as a carrier. Its rate wasadjusted to maintain a constant production rate. The reacting bed ofgrowing polymer particles was maintained in a fluidized state by thecontinuous flow of the make up feed and recycle gas through the reactionzone. A superficial gas velocity of 1-2 ft/sec was used to achieve this.The reactor was operated at a total pressure of 300 psig. To maintain aconstant reactor temperature, the temperature of the recycle gas wascontinuously adjusted up or down to accommodate any changes in the rateof heat generation due to the polymerization.

[0085] The fluidized bed was maintained at a constant height bywithdrawing a portion of the bed at a rate equal to the rate offormation of particulate product. The product was removedsemi-continuously via a series of vanes into a fixed volume chamber,which was simultaneously vented back to the reactor. This allowed forhighly efficient removal of the product, while at the same timerecycling a large portion of the unreacted gases back to the reactor.This product was purged to remove entrained hydrocarbons and treatedwith a small stream of humidified nitrogen to deactivate any tracequantities of residual catalyst. TABLE IV Polymerization Run ConditionsMetallocene Catalyst¹ mixed Zr Bed Weight (kg) 110 Zr (wt %) 0.58 TEALBed Concentration (ppm) 49 Al (wt %) 14.92 Catalyst Productivity (kg/kg)3900 Al/Zr (mole/mole) 87 Bulk Density (g/cc) 0.456 Temperature (° C.)78.9 Average Particle Size (microns) 777 Pressure (bar) 21.7 Melt Index(dg/min) 0.83 Ethylene (mole pct) 50.2 Melt Index Ratio 21.5 Hydrogen(mole ppm) 147 Density (g/cc) 0.9166 Hexene (mole pct) 1.13 Productionrate (kg/br) 33

[0086] This experimental copolymer was an ethylene-hexene copolymerproduced with the mixed zirconocene catalyst described above. Thisexample had the following properties: 0.9187 g/cc density, 0.91 dg/minI₂, 6.53 dg/min I₁₀, 21.1 dg/min I₂₁, 7.18 I₁₀/I₂, 23.2I₂₁/I₂, 31,900M_(n), 98,600 M_(w), 23,1700 M_(z), 3.08 M_(w)/M_(n), 2.35 M_(z)/M_(w),and 10.9 cN melt strength.

Commercial Resins

[0087] Comparative Ex. A is ESCORENE® LD-702 from Exxon Chemical Co., acommercial ethylene-vinyl acetate copolymer (LDPE film resin) having aMelt Index of 0.3 g/10 min a density of 0.943 and a vinyl acetatecontent of 13.3 wt. %. Comparative Ex. B is ESCORENE® LD-1 13 from ExxonChemical Co., a commercial homopolyethylene polymer (LDPE packagingresin) having a Melt Index of 2.3 g/10 min. and a density of 0.921.Comparative Ex. C is EXCEED® 399L60 from Exxon Chemical Co., acommercial ethylene-hexene copolymer (LLDPE blown film resin) having aMelt Index of 0.75 g/10 min. and a density of 0.925. Comparative Ex. Dis AFFNITY® PL-1840 from The Dow Chemical Company, a commercialethylene-octene copolymer (LLDPE blown film resin) having a Melt Indexof 1.0 g/10 min. a density of 0.908 and an octene content of 9.5 wt.%.Comparative Ex. E is ELVAX® 3135 from DuPont Co., a commercialethylene-vinylacetate copolymer (EVA resin for blown film/flexiblepackaging applicatioins ) having Melt Index of 0.3g/10 min. and a vinylacetate content of 12 wt %.

Test Methods

[0088] Melt Index (12) of the resin samples was determined according toASTM-D-1238, Condition E. Melt Flow Rate with a 10 kg top load (I₁₀ wasdetermined according to ASTM-D-1239, Condition N. Melt Flow Rate with a21.6 kg top load (I21) was determined according to ASTM-D1238, conditionF. Density of the resin samples was determined according to ASTM-D-1505.Bulk Density: The resin was poured via a ⅞″ diameter funnel into a fixedvolume cylinder of 400 cc. The bulk density is measured as the weight ofresin divided by 400 cc to give a value in g/cc. Particle Size: Theparticle size was measured by determining the weight of materialcollected on a series of U.S. Standard sieves and determining the weightaverage particle size based on the sieve series used.

Description of Supercritical Fractionation

[0089] The use of supercritical fluids as solvents allows for thefractionation of polymers by either molecular weight or composition. Forexample, supercritical propane is a good solvent for polyethylene andother polyolefins (homo- and copolymers) at high enough pressure andtemperature. If the temperature is kept constant and is high enough sothat the polymer is totally non-crystalline, then one can fractionatethe sample by molecular weight by varying the pressure. The criticalpressure for solubility (that is, the pressure below which the polymeris no longer soluble in the supercritical propane) increases withmolecular weight, so that as the pressure is dropped from some largevalues the higher molecular weight fractions will drop out of solutionfirst, followed by progressively smaller molecular weight fractions asthe pressure is lowered (Watkins, J. J.; Krukonis, V. J.; Condo, P. D.;Pradhan, D.; Ehrlich, P.; J. Supercritical Fluids 1991, 4, 24-31). Onthe other hand, if the pressure is held constant and the temperature islowered, then the most crystallizable portions of the polymer will comeout first. Since for ethylene-a-olefin copolymers the crystallizabilityis generally controlled by the amount of ethylene in the chain, such anisobaric temperature profiling will fractionate the sample bycomposition (Watkins, J. J.; Krukonis, V. J.; Condo, P. D.; Pradhan, D.;Ehrlich, P.; i J. Supercritical Fluids 1991, 4, 24-31; Smith, S. D.;Satkowski, M. M.; Ehrlich, P.; Watkins, J. J.; Krukonis, V. J.; PolymerPreprints 1991, 32(3), 291-292). Thus, one has the option offractionating by either molecular weight or composition from the samesupercritical solution, by varying either pressure or temperature,respectively. In the samples used herein, we chose to obtain fractionsof various molecular weights by isothermal pressure variation.

Supercritical Fractionation Example

[0090] 100 grams of EXPIO resin was fractionated using a supercriticalpropane solution in the manner described above. This was carried out byPhasex Corp., 360 Merrimack St., Lawrence, Mass. 01843. This resulted in14 fractions with the following molecular weights: TABLE V Amount M_(n)M_(w) Fraction (g) (1000 g/mol) (1000 g/mol) M_(w)/M_(n) EXP 10-1 18.50 18.8 88.8 4.72 EXP 10-2 24.62  31.5 87.9 2.79 EXP 10-3 15.76  23.6 85.03.60 EXP 10-4 10.24  17.0 80.9 4.76 EXP 10-5 6.36 14.6 44.1 3.01 EXP10-6 6.51 30.1 62.7 2.08 EXP 10-7 5.93 37.3 72.9 1.96 EXP 10-8 6.65 48.091.9 1.91 EXP 10-9 2.12 63.7 110.  1.73 EXP 10-10 3.30 78.9 128.  1.63EXP 10-11 3.38 88.1 138.  1.56 EXP 10-12 1.83 88.0 146.  1.65 EXP 10-131.98 131.  220.  1.68 EXP 10-14 1.96 145.  268.  1.85 #technique isdiscussed in “Liquid Chromatography of Polymers and Related MaterialsIII” J. Cazes Ed., Marcel Decker, 1981, page 207, which is incorporatedby reference for purposes of U.S. Pat. practice herein. No correctionsfor column spreading were employed; however, data on generally acceptedstandards, e.g. National Bureau of Standards Polyethylene 1475,demonstrated a precision of 0.1 units for M_(w)/M_(n) which wascalculated from elution times. The numerical analyses #were performedusing Expert Ease software available from Waters Corporation.

Comparison of Commercial Polymers with Fractionated Polymer Samples

[0091] TABLE VI η₀ Linear T η₀ Equiv. G_(N) ⁰ η_(ext) Polymer (° C.) (Pa· s) (Pa · s) η₀/η*₁₀₀ (Pa) ratio A--LD-702 190 81740 71 2.3 × 10⁶B--LD-113 190 10000 19 2.3 × 10⁶ C--ECD-399L60 190 10500 3.3 2.3 × 10⁶D--PL-1840 190 20570 12.7 2.3 × 10⁶ E--ELVAX3135 190 45000 45 2.3 × 10⁶4.12 EXP10-Bulk 190  6800 6.7 × 10³ 3.6 2.8  EXP10-9 190 12000 4.9 × 10³5 1.45 × 10⁶  1.43 EXP10-10 190 30000 8.1 × 10³ 9.1 1.7 × 10⁶ 2.5 EXP10-11 190  >4.1 × 10⁴ 1.0 × 10⁴ >9.5 1.9 × 10⁶ 2.22 EXP10-12190 >8.94 × 10⁴ 1.3 × 10⁴ >21 1.74 × 10⁶  3.15 EXP10-13 190 >1.95 × 10⁵5.0 × 10⁴ >33 1.45 × 10⁶  EXP10-14 190 >1.45 × 10⁶ 9.7 × 10⁴ >181 1.3 ×10⁶ # equivalent (same M_(w)) polymer is shown in col. 2 using theequation η₀(190° C.) = 5.62 × 10⁻¹⁴ M_(w) ³³⁶ (Pa · s) derived from Eq.16, Mendelson, et al, J. Poly. Sci., Part A, 8, 105-126. (1970).

Discussion

[0092] Therefore we expect that the multiply branched coomb and H-shapedpolymers of the invention and comb/linear copolymer blends are expectedto exhibit high levels of melt strength at low MIR in view of theirstrain thickening in uniaxial extension. The comb copolymers and theirblends with linear copolymers show strain hardening (even at low levelsof incorporation). Low levels of comb copolymers in a blends with linearpolymer will exhibit little effect on shear thinning (or MIR), but cancause a significant enhancement in strain thickening and melt strength.This gives one the opportunity to design for that combination ofproperties for those applications where it is desirable. The neat combsamples also exhibit the suppression of plateau modulus, asdistinguished from linear copolymers alone, and should be beneficial forextrudability.

We claim:
 1. A polymer composition comprising essentially saturatedhydrocarbon polymers having: A) a backbone chain; B) a plurality ofessentially hydrocarbon sidechains connected to A), said sidechains eachhaving a number-average molecular weight of from 2,500 Daltons to125,000 Daltons and a MWD by SEC of 1.0-3.5; and, C) and a mass ratio ofsidechains molecular mass to backbone molecular mass of from 0.01:1 to100:1.
 2. The hydrocarbon polymer composition of claim 1 wherein saidmass ratio is 0.1:1 to 10:1.
 3. The hydrocarbon polymer composition ofclaim 1 wherein said mass ratio is 0.3:1 to 3:1.
 4. The hydrocarbonpolymer composition of claim 1 wherein said mass ratio is 0.5:1 to 2:1.5. The hydrocarbon polymer composition of claim 1 wherein said backbonechain and said sidechains are derived from one or more of ethylene,propylene, 1-butene, 1-pentene, 1-hexene, 1-octene, 1-decene,1-dodecene, 4-methyl-pentene-1, styrene, alkyl styrenes, norbornene, andalky-substituted norbornenes.
 6. The hydrocarbon polymer composition ofclaim 1 wherein said backbone chain and said sidechains are essentiallyof an ethylene-butene copolymer structure.
 7. The hydrocarbon polymercomposition of claim 1 wherein said backbone chain and said sidechainsare essentially of an ethylene-propylene copolymer structure.
 8. Thehydrocarbon polymer composition of claim 1 wherein said backbone chainand said sidechains are essentially of an ethylene-hexene copolymerstructure.
 9. The hydrocarbon polymer composition of claim 1 whereinsaid backbone chain and said sidechains are essentially of anethylene-octene copolymer structure.
 10. The polymer composition ofclaim 1 comprising 0.1-99.9 wt. %, said essentially saturatedhydrocarbon polymers and 99.9-0.1 wt % essentially linear ethylenecopolymers of weight-average molecular weight from about 25,000 Daltonsto about 500,000 Daltons, and having an MWD of from about 1.75-30 anddensity of 0.85 to 0.96.
 11. A polymer composition comprisingessentially saturated hydrocarbon polymers having: A) a Newtonianlimiting viscosity (η₀) at 190° C. at least 50% greater than that of alinear olefinic polymer of the same chemical composition and weightaverage molecular weight, preferably at least twice as great as that ofsaid linear polymer, B) a ratio of the rubbery plateau modulus at 190°C. to that of a linear polymer of the same chemical composition lessthan 0.5, preferably <0.3, C) a ratio of the Newtonian limitingviscosity (η₀) to the absolute value of the complex viscosity inoscillatory shear (η*)at 100 rad/sec at 190° C. of at least
 5. 12. Thecomposition of claim 11 additionally having D) a ratio of theextensional viscosity measured at a strain rate of 1 sec⁻¹, 190° C., andtime=3 sec (i.e., a strain of 3) to that predicted by linearviscoelasticity at the same temperature and time of 2 or greater. 13.The composition of claim 12 comprising 0.1-99.9 wt. %, said essentiallysaturated hydrocarbon polymers and 99.9-0.1 wt % essentially linearethylene copolymers of weight-average molecular weight from about 25,000Daltons to about 500,000 Daltons, and having an MWD of from about1.75-30 and density of 0.85 to 0.96.
 14. The composition of claim 12comprising 0.3-50 wt %, said essentially saturated hydrocarbon polymersand 50.-99.7 wt % essentially linear ethylene copolymers ofweight-average molecular weight from about 25,000 Daltons to about500,000 Daltons, and having an MWD of from about 1.75-8 and density of0.85-0.93.
 15. The composition of claim 12 comprising 0.3-50 wt %, saidessentially saturated hydrocarbon polymers and 50.-99.7 wt % essentiallylinear ethylene copolymers of weight-average molecular weight from about25,000 Daltons to about 500,000 Daltons, and having an MWD of from about1.75-30 and density of 0.93-0.96.
 16. The composition of claim 12comprising 1.0-5 wt. %, said essentially saturated hydrocarbon polymersand 95-99 wt % essentially linear ethylene copolymers of weight-averagemolecular weight from about 25,000 Daltons to about 500,000 Daltons, andhaving an MWD of from about 1.75-8 and density of 0.85-0.93.
 17. Thecomposition of claim 12 comprising 1.0-5 wt. %, said essentiallysaturated hydrocarbon polymers and 95-99 wt % essentially linearethylene copolymers of weight- average molecular weight from about25,000 Daltons to about 500,000 Daltons, and having an MWD of from about1.75-30 and density of 0.93-0.96.
 18. The composition of claim 12wherein said saturated hydrocarbon polymers consist of a backbone chainand sidechains derived from ethylene alone or ethylene and one or moreof propylene, 1-butene, 1-pentene, 1-hexene, 1-octene, 1-decene,1-dodecene, 4-methyl-pentene-1, styrene, alkyl styrenes, norbomene, andalky-substituted norbornenes.
 19. The composition of claim 18 whereinsaid backbone chain and said sidechains are essentially of anethylene-butene copolymer structure.
 20. The composition of claim 18wherein said backbone chain and said sidechains are essentially of anethylene-hexene copolymer structure.
 21. The composition of claim 18wherein said backbone chain and said sidechains are essentially of anethylene-propylene copolymer structure.